CA2949546C

CA2949546C - Method and apparatus for wastewater treatment using external selection

Info

Publication number: CA2949546C
Application number: CA2949546A
Authority: CA
Inventors: Bernhard Wett; Charles BOTT; Sudhir Murthy; Haydee DE CLIPPELEIR
Original assignee: DC Water and Sewer Authority; Hampton Roads Sanitation District
Current assignee: DC Water and Sewer Authority; Hampton Roads Sanitation District
Priority date: 2014-06-30
Filing date: 2015-06-30
Publication date: 2022-12-13
Anticipated expiration: 2035-06-30
Also published as: MY174371A; RU2017102738A; CN107108291B; US9670083B2; JP2017519630A; JP6983471B2; PH12016502593B1; EP3160911A1; NZ726051A; EP3160911A4; BR112016030233A2; RU2017102738A3; BR112016030233B1; CN107108291A; AU2015284175A1; IL249843A0; ZA201608044B; KR20170026495A; KR20190077100A; US20150376043A1

Abstract

A method and an apparatus for biological wastewater treatment that includes a biological selector and a physical selector. The apparatus comprises an internal biological reactor where wastewater and recycled biomass are combined to provide a high substrate and high electron acceptor gradient for generating morphological biomass features that favor granule formation over floc and filament formation, and an external gravimetric or external screen selector operating on the biomass waste stream for collecting and retaining densified biomass aggregates including dense granule selection and for wasting lighter filaments and flocs. In the method and apparatus, particles may be added to provide cores to promote the formation of aggregates encapsulating the seeded particles. The particles may be added as various materials, for example, in the bioreactor, to initiate or seed the formation of a granule, that could then be separated by or integrated with either the external gravimetric or external screen selector. Further, organisms may be selected for biological phosphorus removal, denitrifying methane oxidizers, biological sulfur or sulfide oxidation, methanogenesis.

Description

METHOD AND APPARATUS FOR WASTEWATER TREATMENT USING
EXTERNAL SELECTION
CROSS REFERENCE TO PRIOR APPLICATION
[0001] <DELETED>.
FIELD OF THE DISCLOSURE

[0002] The present disclosure relates generally to a method and an apparatus for wastewater treatment and, more specifically, to a method and an apparatus for wastewater treatment with size or gravimetric selection.
BACKGROUND OF THE DISCLOSURE

[0003] Aerobic Granular Sludge Processes

[0004] Granular biomass processes for wastewater treatment, were originally limited to anaerobic treatment such as the upflow anaerobic sludge blanket process (UASB), which relies on granular biomass established with a specialty-built upflow reactor to allow symbiotic growth of several different classes of microorganisms, including fermentative, acidogenic, acetogenic, and methogenic. Additional development led to aerobic granular sludge processes being reported in the literature as early as 1997 (Morgenroth E, Sherden T, van Loosdrecht MCM, Heijnen JJ, Wilderer PA. Aerobic granular sludge in a sequencing batch reactor. Water Res 1997; 31:3191-4). These processes are characterized by biomass with a higher density and particle size than flocculent biomass, and to date, have all been accomplished in specialty built reactors, primarily associated with sequencing batch reactors and upflow column reactors or reactors providing high shear conditions. The granular biomass has a particle size ranging from about 0.1-5 mm and a sludge volume index (SVI30 min) less than 35-50 mL/g and a SVIsmin that is similar to the SVI30..
Similarly, aerobic granules have a settling velocity >10 m/h as opposed to approximately 1 m/h for flocculent biomass. The improved settleability of granular sludge over flocculent biomass is one of the important benefits of the method and apparatus according to the instant disclosure.

[0005] One key advantage of aerobic granular sludge is that it can create a niche condition within a granule for any condition that may be needed in separated physical tank volumes.
Flocs and conventional activated sludges are subject to diffusion resistance and aerobic granular sludge can take advantage of relative diffusion resistance inside and outside of a granule to develop and grow different populations simultaneously rather than to promote those conditions within physical tank configurations. A claimed benefit of aerobic granular sludge is that the size of the granule results in substrate and electron acceptor gradients within the granule allowing the accumulation of polyphosphorus accumulating organisms (PAO), glycogen accumulating organisms (GAO), anaerobic ammonia oxidizing bacteria (anammox), and denitrifying heterotrophic bacteria near the center of the granule, while aerobic organisms accumulate near the outside of the granule, including nitrifying bacteria and aerobic heterotrophs.
100061 An example of this approach is further explained below for phosphorus removal.
[0007] Phosphorous Removal [0008] Phosphorus removal from wastewater is typically achieved through either chemical precipitation using iron or aluminum salts or through the application of an anaerobic selector to allow the accumulation of polyphosphate accumulating organisms which provide biological phosphorus removal. Both of these approaches have disadvantages compared to the processes and systems disclosed herein, whereby stable and reliable phosphorus and nitrogen removal can be achieved without the need for a formal anaerobic selector and without chemical precipitation.
[0009] Chemical Phosphorus Removal [0010] Chemicals used for the removal of phosphorus through the formation of precipitates typically include the sulfate or chloride salts of aluminum, ferric iron, and ferrous iron. These chemicals can be added ahead of primary clarification, into the biological process itself (typically activated sludge), or into the primary clarification process, ahead of a tertiary clarification or filtration process. The precipitated phosphorus is then removed from the wastewater flow with the solids stream leaving the primary clarifier, with the waste biomass, with tertiary clarifier solids, or with filter backwash waste, respectively.
Problems with this approach include the need to purchase chemicals, the consumption of alkalinity as a result of adding these chemicals potentially requiring the addition of alkalinity and purchase or more chemical, the generation of additional sludge requiring further treatment and disposal.
[0011] Biological Phosphorus Removal [0012] Biological phosphorus removal (bioP) is well known in the field of wastewater treatment and has the advantages over chemical phosphorus removal of decreased chemical costs, alkalinity demand, and sludge production but suffers from the need for a defined and formal anaerobic zone or period without contamination of dissolved oxygen or oxidized forms of nitrogen (nitrite and nitrate), proper wastewater characteristics in terms of volatile fatty acid (VFA) concentration, and often poor process reliability and upsets.
BioP is generally accomplished by the accumulation of phosphate accumulating organisms (PA0s), SUBSTITUTE SHEET (RULE 26) which store phosphorus as polyphosphate (poly-P) as a source of energy. Under anaerobic conditions, PAOs cleave phosphate groups from poly-P, releasing phosphate to the bulk liquid, and from this obtain energy required to take up VFA. The VFA is stored as an intracellular macromolecule such as polyhydroxybutyrate (PHB). Reducing equivalents are also obtained by PAOs from the degradation of glycogen under anaerobic conditions. Under aerobic conditions, PAO take up phosphate to reform the intracellular poly-P
pool and degrade the stored PHB for growth and energy through normal catabolic and anabolic pathways. Glycogen is also rethrmed under aerobic conditions. The process of bioP is therefore accomplished by subjecting typically flocculent biomass to alternative anaerobic and aerobic conditions according to the schematic shown in Figure 1, which represents a process known commonly as A2/0 or Phoredox and which is capable of both bioP, nitrification, and denitrification. A requirement for this process is a formal anaerobic selector zone with adequate degradable organic material in the form of acetate, or more generally VFA.
[0013] With a proper ratio of VFA to phosphorus, PAOs are able to take up all of the phosphate released in the anaerobic zone and additional phosphate present in the wastewater, achieving a net removal of phosphate through biomass wasting. One challenge associated with the A2/0 process is that nitrate present in the return activated sludge (RAS) stream can enter the anaerobic zone, and this is well known to disrupt the bioP process.
Another aspect of relevance to this disclosure is the ability of some PAO to denitrify (dPAO), whereby nitrate can serve as the electron acceptor instead of oxygen, allowing phosphorus uptake in the anoxic zone. While phosphate uptake by dPAO is known to be significantly slower than under aerobic conditions, the important benefit of maximizing this metabolism is efficiency of use of the same pool of organic carbon in the incoming wastewater for both bioP and nitrogen removal. Limitations of the bioP process include poor reliability in terms of consistent compliance with low effluent total phosphorus limits and strict reliance on the availability of an appropriate quantity of VFA in the incoming wastewater.
[0014] Reactor Configurations for Aerobic Granular Biomass [0015] One such reactor is disclosed in U.S. Pat. No. 5,985,150, which appears to be assigned to Biothane Systems International B.V. In this patent, there is disclosed an airlift reactor providing enhanced shear in which granular sludge is used to treat wastewater. The granular sludge is carried with the upwardly flowing gas into a settling region that applies a relative overflow rate to help in the granular biomass selection process, with return of the underflow to the aerated section of the reactor.
[0016] US Patent No. US 6,566,119 B1 describes an aerobic granular sludge process accomplished in a sequencing batch reactor operated with very short settling and decant periods to select for granular biomass with excellent settling properties.
[0017] US Patent No. US 6,793,822 B2 describes an aerobic granular sludge process for which the granules may be created in a sequencing batch reactor by the methods of, e.g., US

6,566,119 BI, and enhanced by the shear provided by a high superficial gas velocity of the diffused bubble aeration system.
[0018] US Patent Application Publication No. US 2006/0032815 Al discloses an aerobic granular sludge process that appears to have been commercialized as the full-scale Nereda0 process by Royal Haskoning DHV. The features of this sequencing batch reactor aerobic granular sludge process involve wasting of the fraction of slowly settling biomass from the SUBSTITUTE SHEET (RULE 26) process itself and feeding wastewater in an upflow manner through a stagnant and anaerobic layer of settled granules. This allows VFA to diffuse into the granule where PAO and GAO
are established. The process is then aerated to achieve simultaneous nitrification-denitrification and denitrification by dPAO.
[0019] PCT application publication no. WO 2013/151434 Al, which appears to be assigned to Royal Haskoning DHV, discloses the transfer of waste biomass from a granular sludge process, such as that disclosed in, e.g., US 2006/0032815 Al, into a flocculent biomass process, such as the conventional activated sludge process so as to gain the benefits in terms of settleability and nitrogen and phosphorus removal in the activated sludge process.
[0020] While similar to US 2006/0032815 Al, PCT application W02012/175489 Al appears to improve on this process by fluidizing the bed of granules under anaerobic conditions and provides further mixing during the anaerobic period prior to aeration.
[0021] PCT application publication no. WO 2008/141413 Al describes a sequencing batch reactor operated to promote granulation and phosphorus and nitrogen removal, with the added feature that following the anaerobic phosphorus release period, a portion of the reactor contents may be discharged from the reactor to conduct chemical precipitation of phosphate.
External Graximetric Selection for Anammox Granule Formation and Accumulation [0022] US Patent Application Publication No. US 2011/0198284 Al describes the application of an external gravimetric selector for the formation and accumulation of anaerobic ammonia oxidizing bacteria (anammox) containing granules in the process. In this disclosure, it appears that the selection device could be a hydrocyclone, a centrifuge, or a high overflow rate gravity settling device. This disclosure appears to demonstrate the validity of using an SUBSTITUTE SHEET (RULE 26) external gravimetric settling device to select for anammox biomass in either a mainstream or sidestream process.
[0023] External Gravimetric Selection for Settleability Improvement [0024] US Patent Application Publication No. US 2014/0144836 Al describes the use of an external gravimetric selector for the selection of granular biomass in a suspended growth biological wastewater treatment process for the benefit of improved biomass settleability. In this disclosure, it appears that the selection device could be a hydrocyclone, a centrifuge, or a high overflow rate gravity settling device. This disclosure appears to demonstrate the validity of using an external gravimetric settling device to select for biomass with superior settling characteristics.
[0025] Nitrogen and Phosphorus Removal by Struvite Precipitation [0026] Struvite is often formed during anaerobic digestion and in sludge piping, dewatering equipment, and sludge dewatering liquor piping due to high levels of phosphate and ammonia and limiting but sufficient magnesium levels. Often low pH can also limit struvite precipitation. Struvite precipitation and recovery can be used to achieve nitrogen and phosphorus removal, and this has been done using an upflow fluidized reactor with magnesium and alkalinity addition, as disclosed in, e.g., US Patent No. US
7622047 B2.
Furthermore, removal of excess magnesium and phosphorus from anaerobically digested sludge, either through the addition of alkalinity or by aeration to strip excess carbon dioxide and increase pH, and the subsequent recovery of the precipitated struvite, can decrease the risk and extent of unintentional downstream struvite scaling and the associated maintenance requirements.

7 SUBSTITUTE SHEET (RULE 26) [0027] The selection device or method could also be a filter or a screen that selects based on size instead of gravimctric selection SUMMARY OF THE DISCLOSURE
[0028] According to aspects of the disclosure, it is known that granular sludge processes may be implemented in specialty purpose built reactors to achieve efficient biological phosphorus removal, and that external gravimetric selectors may be applied to suspended growth activated sludge processes to achieve biomass densification and/or granulation, so therefore the application of an external gravimetric selector can achieve or enhance biological phosphorus removal through densification or granulation in an activated sludge process. The gravimetric selector could be a hydrocyclone, a centrifuge, a gravity settling device or any gravimetric device that can select based on density. The size selector could be a screen. filter or a membrane. Furthermore the external selector may provide for the accumulation of densified biomass aggregates and granular sludge that achieves a concentration gradient of substrate and electron acceptor that allows for the accumulation of anaerobic space for organisms such as PAO and dPAO near the center of the granule, thus allowing processes such as biological phosphorus removal to be achieved efficiently without purposefully constructed tanks with anaerobic and aerobic selector zones or time sequences.
The meaning of a formal anaerobic zone is that minimal amounts of dissolved oxygen and oxidized forms of nitrogen are present, but that high concentrations of VFA
are present.
However, formation of granules and densified biomass aggregates combines well with the application of anaerobic reactor compartments since enhanced processes requiring an

8 SUBSTITUTE SHEET (RULE 26) anaerobic environment become less vulnerable to oxygen or nitrate introduced into this zone by the return activated sludge (RAS) or internal mixed liquor recycle (MLR) stream.
[0029] According to an aspect of the disclosure an apparatus for biological wastewater treatment is disclosed. The apparatus includes a biological selector and a physical selector.
The apparatus comprises: an internal biological reactor where wastewater and recycled biomass are combined to provide a high substrate and high electron acceptor gradient for generating morphological biomass features that favor granule formation over floc and filament formation; and an external gravimetric or size selector operating on the biomass waste stream for collecting and retaining densified or larger biomass aggregates including dense or larger granule selection and for wasting smaller or lighter filaments and flocs.
[0030] The gravimetric selector may comprise a hydrocyclone, a centrifuge, an external gravity settling device, or any gravimetric approach for separating dense sludge aggregates.
[0031] The size selector may comprise a screen, filter or a membrane device for separating large sludge aggregates.
[0032] The external physical selection promotes the collection and removal of precipitated phosphorus or intracellular polyphosphate as in the case of polyphosphate accumulating organisms.
[0033] The gravimetric selector may promote an electron acceptor and substrate gradient in the densified biomass in order to create an anaerobic or anoxic core for development of niche environments for growing specific organisms.
[0034] The environments may select for organisms for biological phosphorus removal, including aerobic and denitrifying polyphosphate accumulating organisms, glycogen

9 SUBSTITUTE SHEET (RULE 26) accumulation, denitrifying anoxic methane oxidizers, denitrifying biological sulfur or sulfide oxidation, and methanogenesis.
[0035] A formal anaerobic selector is unnecessary to achieve phosphorus removal due to the biological selection provided by the densified aggregates, but the inclusion of a formal anaerobic selector would further improve phosphorus removal performance and reliability.
[0036] A pre-anoxic selector or zone is sufficient to achieve phosphorus removal and the densified aggregate structure of the biomass provides mass transfer resistance for nitrate penetration to the core.
[0037] According to a further aspect of the disclosure, an apparatus is disclosed for the separation of precipitated phosphorus in the form of struvite or calcium-phosphate solids from anaerobically digested or digesting solids using gravimetric selection, with or without supplemental addition of magnesium or calcium or alkalinity, the apparatus comprising a gravimetric selector. The gravimetric selector may comprise a hydrocyclone, a centrifuge, an external gravity settling device, or any gravimetric approach for separating dense sludge aggregates. The size selector may comprise a screen, filter or a membrane device, or any other size selection approach for separating large aggregates.
[0038] The external gravimetric selector may be used to preferentially recover polyhydroxyalkanoates, polyphosphate, inorganic phosphorus-containing minerals, or alginates.
[0039] The external size selector may be used to preferentially recover polyhydroxyalkanoates, polyphosphate, inorganic phosphorus-containing minerals, or alginates.
SUBSTITUTE SHEET (RULE 26) [0040] The apparatus may further comprise a settler and an aeration tank, wherein the internal biological selector is configured in a compartment located between the settler and the aeration tank and the settled sludge is recycled from the settler e.g. by means of drain-pipes at the bottom of the tank to this selector compartment where the wastewater is introduced and from this contact zone the mixed liquor is distributed to the activated sludge tank e.g. by means of distribution pipes at the bottom of the tank.
[0041] According to a further aspect of the disclosure, a method for biological wastewater treatment is disclosed which combines a biological and a physical selector, the method comprising: combining wastewater and recycled biomass in an internal biological reactor to provide a high substrate and high electron acceptor gradient for generating morphological biomass features that favor granule formation over floc and filament formation; and operating an external gravimetric or size selector on the biomass waste stream for collecting and retaining densified or large biomass aggregates including dense granule selection and for wasting lighter filaments and flocs.
[0042] The method may further comprise implementing the external physical selection to promote the collection and removal of precipitated phosphorus or intracellular polyphosphate as in the case of polyphosphate accumulating organisms.
[0043] The method may further comprise implementing the gravimetric or size selection process to promote an electron acceptor and substrate gradient in the densified or large biomass in order to create an anaerobic or anoxic core for development of niche environments for growing specific organisms.
[0044] The environments may select for organisms for biological phosphorus removal, including aerobic and denitrifying polyphosphate accumulating organisms, glycogen SUBSTITUTE SHEET (RULE 26) accumulation, denitrifying anoxic methane oxidizers, denitrifying biological sulfur or sulfide oxidation, and methanogenesis.
[0045] According to a still further aspect, a method is disclosed for the separation of precipitated phosphorus in the form of struvite or calcium-phosphate solids from anaerobically digested or digesting solids using gravimetric selection, with or without supplemental addition of magnesium or calcium or alkalinity.
[0046] According to a still further aspect, an apparatus for biological wastewater treatment is disclosed that includes a biological selector and a physical selector, where the apparatus comprises:
an internal biological reactor where wastewater and recycled biomass are combined to provide a high substrate and high electron acceptor gradient for generating morphological biomass features that favor granule formation over floc and filament formation; and an external screen selector operating on the biomass waste stream to collect and retain larger sized sludge aggregates out of the waste stream that favor non-compressible granule selection and to waste compressible filament and flocs.
[0047] The morphology promotes an electron acceptor and substrate gradient in order to create an anaerobic or anoxic core for development of niche environments for growing specific organisms.
[0048] The morphology promotes an electron acceptor and substrate gradient in order to allow for proximate substrate or metabolite transfer across niche environments.
[0049] The selection promotes for collection and removal of precipitated phosphorus.
[0050] According to a still further aspect of the disclosure, an apparatus is disclosed for the separation of precipitated phosphorus in the form of struvite or calcium-phosphate solids from anaerobically digested or digesting solids via an external screen selector, with or Date Recue/Date Received 2021-02-05 without supplemental addition of magnesium or calcium or alkalinity, the apparatus comprising: an external screen selector that collects and retains larger sized sludge aggregates out of a waste stream that favor non-compressible granule selection and that wastes compressible filament and flocs.
[0051] The environments select for organisms for biological phosphorus removal, denitrifying methane oxidizers, biological sulfur or sulfide oxidation, methanogenesis.
BRIEF DESCRIPTION OF THE DRAWINGS
[0052] Fig 1 shows an example of a process flow diagram for a known A2/0 system.
[0053] Fig 2 shows an example of an A2/0 system with an external gravimetric selector in the form of a hydrocyclone, according to an aspect of the disclosure.
[0054] Fig 3 shows an example of an MLE system with an external gravimetric selector in the form of a hydrocyclone, according to a further aspect of the disclosure.
[0055] Fig 4 shows an example of an MLE system with an alternative external gravimetric selector in the form of a hydrocyclone, according to a still further aspect of the disclosure.
[0056] Fig 5 shows an example of a combined integral clarifier-biological activated sludge system with anaerobic selector and an external gravimetric selector in the form of a hydrocyelone.
[0057] Fig 6 shows an example of an impact of a hydrocyclone operation on bioP, and transition from predominantly chemical P precipitation to biological P
removal, according to principles of the disclosure.

SUBSTITUTE SHEET (RULE 26) [0058] Fig 7 shows an example of an impact of a hydrocyclone operation on bioP, and step-wise decrease of metal addition for chemical P removal down to a zero-dosing rate, according to principles of the disclosure.
[0059] Fig 8 shows an example of an impact of a hydrocyclone operation on bioP, where P
content in activated sludge biomass is in the range of 2.8 to 4.5% in the mixed liquor volatile suspended solids (MLVSS) in the mainstream and 1.3 to 2.3% in the sidestream process, according to principles of the disclosure.
[0060] Figs 9A to 9C show three perspective views of one example embodiment of a screening apparatus that may be included for size selection in lieu of the external gravimetric selector of the instant disclosure.
DETAILED DESCRIPTION OF THE DISCLOSURE
[0061] The disclosure and the various features and advantageous details thereof are explained more fully with reference to the non-limiting embodiments and examples that are described andlor illustrated in the accompanying drawings and detailed in the following description and attachment. It should be noted that the features illustrated in the drawings and attachment are not necessarily drawn to scale, and features of one embodiment may be employed with other embodiments as the skilled artisan would recognize, even if not explicitly stated herein. Descriptions of well-known components and processing techniques may be omitted so as to not unnecessarily obscure the embodiments of the disclosure. The examples used herein are intended merely to facilitate an understanding of ways in which the disclosure may be practiced and to further enable those of skill in the art to practice the embodiments of the disclosure. Accordingly, the examples and embodiments herein should SUBSTITUTE SHEET (RULE 26) not be construed as limiting the scope of the disclosure. Moreover, it is noted that like reference numerals represent similar parts throughout the several views of the drawings.
[0062] The terms "including," "comprising" and variations thereof, as used in this disclosure, mean "including, but not limited to," unless expressly specified otherwise.
[0063] The terms "a," "an," and "the," as used in this disclosure, means "one or more", unless expressly specified otherwise.
[0064] Devices that are in communication with each other need not be in continuous communication with each other, unless expressly specified otherwise. In addition, devices that are in communication with each other may communicate directly or indirectly through one or more intermediaries.
[0065] Although process steps, method steps, algorithms, or the like, may be described in a sequential order, such processes, methods and algorithms may be configured to work in alternate orders. In other words, any sequence or order of steps that may be described does not necessarily indicate a requirement that the steps be performed in that order. The steps of the processes, methods or algorithms described herein may be performed in any order practical. Further, some steps may be performed simultaneously.
[0066] When a single device or article is described herein, it will be readily apparent that more than one device or article may be used in place of a single device or article. Similarly, where more than one device or article is described herein, it will be readily apparent that a single device or article may be used in place of the more than one device or article. The functionality or the features of a device may be alternatively embodied by one or more other devices which are not explicitly described as having such functionality or features.
SUBSTITUTE SHEET (RULE 26) [0067] FIG 1 shows an example of a known A210 activated sludge processing system 100 (and process). The system 100 comprises a primary clarifier 110, an anaerobic zone 120, an anoxic zone 130, an aerobic zone 140, a separator or secondary clarifier 150, and a plurality of pumps 160, 170, 180.
[0068] The system 100 may include pretreatment (not shown), which may include a bar screen (not shown), a grit remover (not shown), a pre-treatment chamber (not shown), and an influent pump (not shown). The system 100 may receive wastewater 105 from an external source (not shown), such as, e.g., a sewage system, and process the wastewater 105 in the pretreatment stage to remove larger objects such as cans, rags, sticks, plastic packets, and the like, from the wastewater 105. The pretreatment stage may also include a pre-treatment chamber (not shown), which may contain, e.g., a sand or grit chamber, to adjust the velocity of the incoming wastewater 105 and thereby allow the settlement of, e.g., sand, grit, stones, broken glass, and the like. The pretreatment stage may further include a tank (not shown) for removal of, e.g., fat, grease, and the like.
[0069] Following the pretreatment stage (not shown), the remaining solid-liquid mixture 105, which includes excess wastewater containing accumulated solids, may be sent to the primary clarifier 110 for gravity settling. The primary clarifier 110 may include a tank (e.g., a clarifier tank, a sediment tank, etc.), which may have one of a variety of shapes, such as, e.g., rectangular, cone shape, circular, elliptical, and so on. The primary clarifier 110 may have a chemical or ballast material added to improve solids removal. The primary clarifier 110 settles the heavier solids from the solid-liquid mixture 105. The resulting underflow (not shown) may be output from the primary clarifier 110 and sent to solids handling for further treatment, such as, e.g., thickening, stabilization, conditioning, dewatering, sludge SUBSTITUTE SHEET (RULE 26) processing, and so on, as is known by those having ordinary skill in the art.
The resulting output 115 from the primary clarifier may be fed to the anaerobic zone 120, anoxic zone 130 and aerobic zone 140 for further processing before being fed as a stream 145 to the separator 150. The output 145 from the aerobic zone may be pumped by MLR pump 160 to the anoxic zone 130 via MLR pump output 165. An underflow from the separator 150 may be fed back to an input of the anaerobic zone by RAS pump 170 via an RAS pump output line 175. The underflow may also be output from the separator 150 fed and sent out by WAS
pump 180 to, e.g., solids handling for further treatment, such as, e.g., thickening, stabilization, conditioning, dewatering, sludge processing, and so on, as is known by those having ordinary skill in the art. and the remainder may be output from the separator 150 at an output 155.
[0070] The system 100 is capable of carrying out biological phosphorus removal, nitrification and denitrification. BioP reliability in this system (and process) may be problematic due to the transfer of nitrate present in the return activated sludge stream 175 (RAS) to the anaerobic zone 120.
[0071] FIG 2 illustrates an example of an A20 activated sludge processing system 200 (and process), according to principles of the disclosure. Further to the system 100 shown in FIG 1, the system 200 includes a gravimetric selector 260 that is in fluid communication with the aerobic zone 140 via a pump 250 and lines 245, 265. An output 285 of the gravimetric selector may be coupled to further processing components (not shown) for further treatment, such as, e.g., solids handling, including, e.g., thickening, stabilization, conditioning, dewatering, sludge processing, and so on.
[0072] As seen in FIG 2, the waste stream 245 may be taken directly from the aerobic zone 140 (e.g., directly from a reactor tank (not shown)) and applied to the external gravimetric selector 260 via the pump 250 for granular densified biomass production. The gravimetric selector 260 may include, e.g., a hydrocyclone, or the like. The more dense and larger particles 265 may be returned from the gravimetric selector 260 to the aerobic zone (e.g., a reactor (not shown)) and the lighter fraction 285, representing the wasted solids, may be taken from the system 200. The inclusion and implementation of the gravimetric selector 260 enhances bioP performance and improves the reliability of the system 100 (shown in FIG. 1).
[0073] Figs 9A to 9C show three perspective views of one example embodiment of a screening, filtering or membrane apparatus 10 that is an external size selector and may be included in the external gravimetric selector 260 of the instant disclosure.
[0074] Referring to Figs 9A to 9C, the gravimetric selector 260 may include, e.g., a screening, filtering or membrane apparatus 10 that is configured to receive the waste stream 1 (or wastewater stream 245 in Fig 2) and segregate the stream via an internal particle/solids separator 2 into waste constituents to be output to a waste stream 3 (or WAS
285 in Fig 2) and those waste constituents to be retained 4 (or 265 in Fig 2). The screening, filtering or membrane apparatus 10 may segregate the stream based on size and compressibility versus densification.
[0075] An optional screen wash 5 using gas, liquid or some combination of matter can be added to further assist in the screening process. This screen wash 5 can be directed toward the screen 2 in a variety of different ways, which differently affect the solids retention time, including but not limited to, along the vertical axis (Fig 9A), angle directly perpendicular to the screen (Fig 9B), or along the horizontal axis (Fig 9C).

[0076] In the system 100 (shown in Fig 1) or system 200 (shown in Fig 2), particles may be added to provide cores to promote the formation of aggregates encapsulating the seeded particles. The particles may be added as various materials, for example, in the bioreactor to initiate or seed the formation of a granule, that could then be separated by or integrated with either an external gravimetric or external screen.
[0077] Further, organisms may be selected in the system 100 (or 200) for biological phosphorus removal, denitrifying methane oxidizers, biological sulfur or sulfide oxidation, methanogenesis.
[0078] U.S. Patent Application Publication No. US 2014/013273 discloses an example of a method and apparatus for selecting and retaining solids in an activated sludge process for improving wastewater treatment using screens that may be used in the gravimetric selector 260 of the instant disclosure.
[0079] FIG 3 shows an example of a Modified Ludzack-Ettinger (MLE) activated sludge processing system 300 (and process). according to principles of the disclosure. Further to the system 200 shown in FIG 2, the system 300 does not include an anaerobic zone 120. Accordingly, the output stream 115 from the primary clarifier 110 is fed directly to the anoxic zone 130.
Without the gravimetric selector 260, the system 300 is capable of only nitrification and denitrification, and bioP activity may be limited or nonexistent. With the gravimetric selector 260 in the system 300 (e.g., in the configuration shown in FIG 3), the system provides granular biomass production with return of more dense and larger particles 265 to the aerobic zone 140 (e.g., the reactor (not shown)) and the lighter fraction 285 representing the wasted solids taken from the system 300. The system 300 provides reliable and consistent bioP by, e.g., providing an ecological niche near the center of the granular biomass particles, where PAO
and dPAO are capable of being accumulated.
[0080] FIG 4 shows an example of a system 400 that is similar to the system 300 shown in FIG 3, with all the same advantages, but the external gravimetric selector 260 is applied to the return activated sludge stream 175 as opposed to the aerobic zone 140 (e.g., the aeration tank biomass (not shown) in the aerobic zone 140).
[0081] FIG 5 shows an example of a combined integral clarifier-biological activated sludge process with anaerobic selector and an external gravimetric selector in the form of a hydrocyclone. The added external gravimetric selector improves bioP
performance by combining biological selection through the use of a standard anaerobic selector with physical selection through the novel application of the external gravimetric selector.
[0082] FIG 6 shows an example of the impact of the external gravimetric selector in, e.g., the system 300 (or 200 or 400). In particular, FIG 6 shows the impact of a hydrocyclone gravimetric selector on bioP at the Strass wastewater treatment plant, which uses a MLE
process as shown in FIG 3, including a hydrocyclone biomass wasting system.
The data show the decreased reliance on chemical phosphorus removal with a progressive increase in biological phosphorus removal efficiency and reliability. The addition of sodium aluminate for chemical P removal was completely eliminated.
[0083] FIG 7 shows an example of the reduction in sodium aluminate dosing at the Strass wastewater treatment plant using the system 200 (or 300 or 400) for biomass wasting.
[0084] FIG 8 shows an example of the impact of the hydrocyclonc operation at the Strass wastewater treatment plant on bioP using, e.g., the system 200 (or 300 or 400). During experiments, the P content of biomass samples collected increased to values typical of SUBSTITUTE SHEET (RULE 26) conventional bioP plants. This was significant because the Strass plant does not have anaerobic selectors in place. Conventional non-bioP biomass is expected to contain approximately 1.5 to 2.0% PALVSS. The data in FIG 8 show the P content in activated sludge biomass in the range of 2.8 to 4.5% P/MLVSS in the mainstream in the sidestream process.
[0085] Thus, as evident from the foregoing, for plants with no anaerobic selector, an external gravimetric selector can result in bioP. However, for plants that already have an anaerobic selector and designed for bioP (have biological selection) the addition of an external gravimetric selector can improve the reliability and efficiency of bioP
[0086] The disclosure provides for a system that may combine biological (with anaerobic selector) and physical selection (with external selector).
[0087] According to principles of the disclosure, selection of more dense granules as a result of an external gravimetric selector provides a good ecological niche for dPAO and PAO, which are themselves more dense due to polyphosphate granules, so granule formation through an external gravimetric selector provides another ability to accumulate and physically select for PAO and dPAO, and PAO and dPAO have higher density due to polyphosphate granules and therefore the gravimetric selector (e.g., hydrocyclone) can select for these organisms more efficiently.
[0088] Compared to, e.g., the system 100 shown in FIG 1, an external gravimetric selector provides better selection of dPAO over PAO because during aerated periods or in aerated zones, the inside of the granule is protected from high bulk DO, but nitrate can be present as a result of production by nitrification and diffusion to the inside of the granule. This makes nitrate is available for dPAO, providing a benefit in that VFA are being used for both N and SUBSTITUTE SHEET (RULE 26) P removal, which results in more efficient use of wastewater carbon for N and P removal than conventional processes where dPAO activity is usually a small fraction of PAO activity.
[0089] In an experiment being conducted at the WWTP Strass plant according to the principles of the instant disclosure, the main biological treatment provides high-rate carbon removal in an up-stream A-stage (not shown) at low sludge retention time (SRT) and mainly nitrogen removal in a downstream low SRT system (B-stage, not shown). The B-stage consists of 2 treatment lanes each with 2 carousel-type tanks in series which are all equipped with diffusers. Depending on the on-line measured ammonia and nitrate concentrations at the effluent of the activated sludge tanks the aeration is controlled to achieve a certain DO-set-point and nitrification efficiency. The second tank (not shown) in series is predominantly aerated in order to supply oxygen to the nitrifying biomass and the first tank (not shown) in series is mostly unacrated to provide an anoxic environment to heterotrophic biomass to denitrify recycled nitrate (MLE-mode). When the ammonia concentration increases close to limit values, the first tank may get aerated and serve as a swing-zone with additional nitrification capacity.
[0090] The initial design at the VVWTP Strass plant relies on chemical P-removal by metal dosing and does not target biological phosphorus removal since no anaerobic zone is implemented and most organic acids are already removed in the A-stage and therefore are lacking for any bio-P activity. Recently for the improvement of the efficiency of the nitrogen removal process anammox granules have been augmented from the sidestream treatment system for sludge liquors (DEMON -process) and retained in the mainstream system by the use of hydrocyclones according to the disclosure of US Patent Application No. US
2011/0198284 Al. As described in published patent application, the cyclones may be used not only to retain anammox granules but also to create and to select for more dense activated sludge flocs in order to provide environmental niches for PAOs and DPAOs and to enhance bio-P activity. Then the metal dosing rate may be step-wise decreased (e.g., as shown in FIG 6) while maintaining low effluent ammonia concentrations below the limit value of, e.g., 1 mg P/L. In at least one experiment, the dosing rate was set to zero and a concentration decrease resulted from about ca. 5 mgPiL down to 1 mgP/L exclusively by the biological process due to continued operation of the gravimetrical selector. Measurements indicating a 3% to 4.5%
P-content in VSS of the biomass (e.g., shown in FIG 8) clearly confirmed high phosphorus accumulating capabilities.
[0091] According to the principles of this disclosure, the bio-P activity of more dense sludge aggregates selected by the gravimetric selector (e.g., hydrocyclone) may be significantly enhanced even without any dedicated anaerobic reactor zone.
Further, the combination of a gravimetrical selector with an anaerobic zone, serving as a biological selector, further enhances bio-P activity where, e.g., denser biomass aggregates may come into contact with concentrated wastewater directly from the sewer or from a pre-treatment process. Anaerobic VFA up-take and storage promotes the generation of more dense biomass which again allows the accumulation of these aggregates by the physical selection process out of the waste stream. Such an anaerobic zone could be implemented upstream at, e.g., the up-front end of the biological process where the wastewater is fed to the activated sludge system (as shown, e.g., in FIG 2).
[0092] Alternatively the anaerobic zone could be configured in, e.g., a compartment positioned between settlers and one or more aeration tanks, as shown, e.g., in FIG 5. The SUBSTITUTE SHEET (RULE 26) settled sludge may be recycled from the settler, e.g., by means of drain-pipes provided at the bottom of the tank. The settled sludge may be fed by, e.g., the drain-pipes, to the anaerobic compartment, where the wastewater may be introduced, and from this contact zone the mixed liquor may be distributed to the activated sludge tank, e.g., eventually by means of distribution pipes at the bottom of the tank (e.g., as shown in FIG 5). This implementation may be compatible with, e.g., the BIOCOS process described in WO/2011/091452 and/or WO/2001/046075 which already include configured alternating settling tanks with sludge-recycle-pipes at the bottom of the settlers and air-lift (mammoth pumps) providing the suction pressure to these drain pipes.
[0093] Additionally, the system may include multiple walls (e.g., dual-walls) between settlers and aeration tank in order to provide a separate compartment where the thickened sludge may come into contact with the feed and the pressure head (not shown) of, e.g., an air-lift pump (not shown) that may be used to distribute the mixed liquor to the bottom of the aeration tank. During cycle phases when the air-lift pump is not operated the continued feed-flow may be introduced to the contact-compartment and supply substrate to the high-solids liquor.
[0094] While the disclosure has been described in terms of exemplary embodiments, those skilled in the art will recognize that the disclosure can be practiced with modifications in the spirit and scope of the appended claims. These examples are merely illustrative and are not meant to be an exhaustive list of all possible designs, embodiments, applications or modifications of the disclosure.

Claims

WHAT IS CLAIMED IS:

1. A method for biological wastewater treatment utilizing a biological reactor, the method comprising:
combining wastewater and a recycled biomass in the biological reactor to provide a concentration gradient of substrate and electron acceptor for generating morphological biomass features that favor granule formation over floc and filament formation;
outputting, from the biological reactor, a stream comprising granular or densified biomass;
supplying the stream comprising the granular or densified biomass to a separator;
outputting, from the separator, an underflow or a retained fraction comprising the granular or densified biomass;
supplying the underflow to a return activated sludge (RAS) stream and to a physical selector comprising a hydrocyclone or a screening apparatus;
operating the physical selector comprising the hydrocyclone or screening apparatus on the underflow or retained fraction to collect the granular or densified biomass and to waste smaller or lighter filaments and floc;
supplying the collected granular or densified biomass to the return activated (RAS) stream;
supplying, by operation of a pump, the return activated sludge (RAS) stream, including the collected granular or densified biomass, to the biological reactor as a recycled stream to provide the recycled biomass; and providing a pre-anoxic selector or zone that achieves phosphorus removal and a densified aggregate structure in the granular or densified biomass.
Date Recue/Date Received 2022-02-08

2. The method of claim 1, further comprising:
separating precipitated phosphorus or intracellular polyphosphate from solids.

3. The method of claims 1 to 2, further comprising:
adding particles to provide cores to promote formation of aggregates encapsulating the particles.

4. The method of any one of claims 1 to 3, further comprising:
promoting an electron acceptor and substrate gradient in the densified biomass in order to create an anaerobic or anoxic core for development of a niche environment for growing a specific organism, wherein the specific organism is selected for biological phosphorus removal, including aerobic and denitrifying polyphosphate accumulating organisms, glycogen accumulation, denitrifying anoxic methane oxidizers, denitrifying biological sulfur or sulfide oxidation, and methanogenesis.

5. The method of any one of claims 1 to 4, further comprising operating an anaerobic selector or zone to improve phosphorus removal performance and reliability.

6. The method of any one of claims 1 to 5, further comprising recovering by the physical selector polyhydroxyalkanoates, polyphosphate, inorganic phosphorus-containing minerals, or alginates in the underflow or retained fraction.

Date Recue/Date Received 2022-02-08

7. A method for biological wastewater utilizing a biological reactor, the method comprising:
combining wastewater and a recycled granular or densified biomass in the biological reactor to provide a concentration gradient of substrate and electron acceptor for generating morphological biomass features that favor granule formation over floc and filament formation;
outputting a biomass waste stream from the biological reactor;
supplying the biomass waste stream from the biological reactor to a separator;
extracting an underflow from the separator and supplying the extracted underflow to a return activated sludge (RAS) line and an input of a physical selector that comprises a hydrocyclone or a screening apparatus, wherein the underflow includes a granular or densified biomass;
operating the physical selector on the input underflow to collect and retain the granular or densified biomass and to waste flocs or filaments;
returning the collected granular or densified biomass from the selector to the biological reactor as the recycled granular or densified biomass; and providing a pre-anoxic selector or zone that achieves phosphorus removal and a densified aggregate structure in the granular or densified biomass.

8. The method of claim 7, further comprising:
separating precipitated phosphorus or intracellular polyphosphate from solids.

9. The method of claim 7 or 8, further comprising:

Date Recue/Date Received 2022-02-08 adding particles to provide cores to promote formation of aggregates encapsulating the particles.

10. The method of any one of claims 7 to 9, further comprising:
promoting an electron acceptor and substrate gradient in the densified biomass in order to create an anaerobic or anoxic core for development of a niche environment for growing a specific organism, wherein the specific organism is selected for biological phosphorus removal, including aerobic and denitrifying polyphosphate accumulating organisms, glycogen accumulation, denitrifying anoxic methane oxidizers, denitrifying biological sulfur or sulfide oxidation, and methanogenesis.

11. The method of any one of claims 7 to 10, further comprising operating an anaerobic selector to improve phosphorus removal performance and reliability.

12. The method of any one of claims 7 to 11, further comprising recovering by the physical selector polyhydroxyalkanoates, polyphosphate, inorganic phosphorus-containing minerals, or alginates in the underflow.

Date Recue/Date Received 2022-02-08